Device for removing organic matters in acidic high-salt leaching liquor of fly ash

Abstract

A fly ash acidic high-salt leaching solution organic matter removal device comprises a box body, a Fenton reaction zone and an activated carbon regeneration / adsorption zone located below the Fenton reaction zone are arranged in the box body, one side of the Fenton reaction zone is connected with a dosing device, a plurality of shuttle valves are arranged on the other side of the Fenton reaction zone, and a siphon pipe is arranged to penetrate into the Fenton reaction zone. The bottom shuttle valve is connected with the slender straight pipe A, and the top shuttle valve is connected with the slender straight pipe B; the activated carbon adsorption area is composed of a plurality of filter layers, a slender straight pipe A extends into the capillary effect layer, and a slender straight pipe B extends into the regenerated liquid distributor. According to the acid salt wastewater treatment device, organic matters in acid salt wastewater are removed under the combined action of adsorption and Fenton oxidation processes, and meanwhile, an activated carbon adsorption material can be regenerated, so that the cyclic utilization of an adsorbent is realized, and the treatment cost is reduced.

Description

Technical Field

[0001] The invention belongs to the technical field of waste incineration fly ash treatment, and particularly relates to a device for removing organic matter from fly ash acidic high-salt leaching liquid. Background Art

[0002] Waste incineration fly ash contains a high proportion of chloride salts. During the wet pretreatment process, a large amount of soluble chloride salts enter the liquid phase, forming high-salinity wastewater. The inorganic salt components NaCl, KCl, and CaCl2 contained in this wastewater have high recycling value. Currently, the treatment methods for this high-salinity wastewater mainly use technologies such as multi-effect evaporation, MVR evaporation, multi-stage flash evaporation, membrane distillation, electrodialysis, and ion-exchange membrane electrolysis for resource recovery. Diaphragm electrolysis generally requires the organic matter concentration (TOC) in the salt solution to be no higher than 200 mg / L, while ion-exchange membrane electrolysis has even stricter TOC requirements for the influent. The "Three-Year Action Plan for the 'Zero Landfill' of Hazardous Waste in Zhejiang Province" proposes a pilot control indicator for the resource utilization of by-product salt in Zhejiang Province, setting a TOC control limit of ≤70 mg / kg for industrial waste salt and ash washing waste salt that can be used as by-products. Therefore, the organic matter concentration must be controlled before the evaporation desalination process. Otherwise, the organic matter concentration in the high-salinity organic wastewater will be too high, which will be detrimental to the resource recovery of the salt.

[0003] Fenton oxidation technology is a highly efficient advanced oxidation process (AOPs) that is widely used in wastewater treatment, especially for refractory organic pollutants. The core of this technology is to use ferrous ions (Fe 2+ ) acts as a catalyst to react with hydrogen peroxide (H2O2) to produce highly active hydroxyl radicals (·OH) under acidic pH conditions (usually pH < 3). Its redox potential is as high as +2.8eV, which can indiscriminately attack and degrade organic molecules in wastewater, achieving rapid mineralization of pollutants.

[0004] However, the non-selective nature of hydroxyl radicals also means that they may react with other ions in wastewater, such as chloride ions (Cl - ) reacts to form chlorine radicals (Cl·), which compete with organic pollutants for hydroxyl radicals, thereby affecting the removal efficiency of organic matter in the Fenton process. This phenomenon is particularly evident in the treatment of high-salinity wastewater, because high concentrations of chloride ions may significantly reduce the effective concentration of hydroxyl radicals.

[0005] As a porous adsorption material, activated carbon exhibits excellent adsorption properties with its unique two-dimensional spatial structure and rich surface functional groups, and can effectively remove organic matter from wastewater. The pore structure of activated carbon provides a large number of adsorption sites for pollutants, while the functional groups on its surface enhance the adsorption capacity of specific organic molecules through chemical reactions. However, the adsorption capacity of activated carbon is limited. Once it reaches saturation, it needs to be regenerated or replaced, which undoubtedly increases treatment costs and operational complexity.

[0006] Given the limitations of single technologies in treating complex wastewater, researchers have begun exploring complex treatment processes in recent years that combine Fenton oxidation with other technologies such as activated carbon adsorption, biological treatment, and membrane separation. This combined process not only improves pollutant removal efficiency but also enables resource recycling, reduces overall treatment costs, and improves the sustainability of wastewater treatment. For example, activated carbon can be used as a post-treatment step in the Fenton reaction to remove residual organic matter and heavy metal ions, or activated carbon can be used as a pretreatment step before the Fenton reaction to reduce the ineffective consumption of hydroxyl radicals during the reaction.

[0007] Chinese patent publication number CN215975303 U, publication date March 8, 2022, the name of the invention is a rural water purification equipment suitable for surface water sources in mountainous areas. The application discloses a rural water purification equipment suitable for surface water sources in mountainous areas, including a box body, in which a coagulation area, a sedimentation area, a filtration area, a disinfection area, and a clear water area are connected in sequence from top to bottom. However, the invention has some limitations in practical applications. First, the activated carbon adsorption material used in the filtration area needs to be replaced after adsorption saturation, which not only increases the material cost, but also the treatment of the replaced activated carbon also brings environmental problems, increases the processing cost and operation complexity. Secondly, the dosing equipment only includes a dosing pipe connected to an external dosing box. The design is relatively simple. The operator is required to mix the flocculant in proportion in advance and then manually add it to the equipment, which undoubtedly increases the complexity and labor intensity of the operation.

[0008] To achieve the removal of organic matter from fly ash acidic high-salt wastewater, reduce the number of steps during dosing operations, and ensure the quality of subsequent MVR evaporation and crystallization to recover industrial by-product salt, the present invention proposes a high-efficiency integrated device. This device facilitates dosing operations, removes organic matter from the acidic high-salt extract, and can regenerate activated carbon adsorption materials, reducing disposal costs. The effluent from the equipment can directly enter the MVR evaporation system without the need for pH readjustment. Utility Model Content

[0009] The technical problem to be solved by the present invention is to address the above-mentioned deficiencies in the prior art. The purpose of the present invention is to provide a device for removing organic matter from fly ash acidic high-salt leachate by using the method of Fenton oxidation + activated carbon adsorption / regeneration + acid-base neutralization and ensuring the water quality of the MVR evaporator inlet water.

[0010] To achieve the above objectives, the present invention provides a device for removing organic matter from fly ash acidic, high-salt extracts. The device comprises a housing containing a Fenton reaction zone and an activated carbon adsorption zone located below the Fenton reaction zone. The Fenton reaction zone is connected to a dosing device on one side and to several shuttle valves on the other side. A siphon tube extends into the Fenton reaction zone, and a sedimentation hopper is located at the bottom of the Fenton reaction zone. The bottom shuttle valve is connected to a slender straight tube A, while the top shuttle valve is connected to a slender straight tube B. The activated carbon adsorption zone comprises several filter layers, with slender straight tube A extending into the capillary effect layer and slender straight tube B extending into the regeneration liquid distributor.

[0011] Furthermore, a check block is provided in each shuttle valve, the top shuttle valve is connected to a regeneration liquid siphon, and the bottom shuttle valve is connected to a water inlet of the Fenton reaction zone.

[0012] Furthermore, the dosing device includes a plurality of dosing ports, a water jet inlet pipe and a plurality of dispersion discs, the plurality of dosing ports are connected through the water jet inlet pipe, and the water jet inlet pipe and the plurality of dispersion discs are connected through a U-shaped connecting pipe.

[0013] Furthermore, a plurality of dispersion discs in the dosing device extend deep into the Fenton reaction zone.

[0014] Furthermore, the Fenton reaction outlet is connected to a siphon tube, and the bottom end of the siphon tube is located above the sedimentation sludge hopper.

[0015] Furthermore, an acid-base neutralizer dosing port and a pH online monitor are provided on the top of the Fenton reaction zone.

[0016] Furthermore, a sedimentation zone is provided at the bottom of the Fenton reaction zone, including a sedimentation sludge hopper and a sludge discharge pipe connected below the sedimentation sludge hopper.

[0017] Furthermore, the plurality of filter layers include a water distribution layer, an activated carbon adsorption layer and a fiber constant temperature layer provided on the bottom end of the box body, the activated carbon adsorption area is composed of a plurality of filter layers, and the capillary effect layer is located below the regeneration liquid distributor.

[0018] Furthermore, the water inlet distribution layer is located at the bottom of the plurality of filter layers, one end of the layer is connected to the activated carbon regeneration liquid outlet, and the other end is connected to the equipment water inlet device.

[0019] Beneficial Effects: The combined action of adsorption and Fenton oxidation processes removes organic matter from the acidic, high-salt extract, while also regenerating the activated carbon adsorption material, enabling the recycling of the adsorbent and reducing treatment costs. Gravity sedimentation is used to separate the solid and liquid iron sludge produced after the pH of the acidic, high-salt extract is adjusted, ensuring that the effluent salt solution meets the requirements for entry into the MVR evaporator. Furthermore, the capillary effect and siphon principle are utilized to achieve intermittent reaction, reducing mechanized power consumption. The Fenton reaction dosing device achieves efficient and rapid mixing of the catalyst and oxidant, enhancing reaction efficiency and reducing reagent consumption. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] Figure 1 The present invention is a schematic diagram of the structure of a device for removing organic matter from fly ash acidic high-salt leaching solution.

[0021] Figure 2 It is a structural diagram of the regeneration liquid distributor.

[0022] Figure 3 It is a schematic diagram of the heating tube structure in the constant temperature zone of fiber filter material.

[0023] In the figure: 1 vacuum circulation pump, 2 circulation pump water inlet, 2-1 equipment water inlet stop valve, 3 activated carbon adsorption / regeneration module, 3-1 water inlet distribution layer, 3-1.1 activated carbon regeneration liquid outlet, 3-1.2 stop valve, 3-2 activated carbon adsorption layer, 3-3 fiber filter material constant temperature layer, 3-3.1 electric heating tube, 3-3.2 electric heating center, 3-4 capillary effect layer, 4 slender straight tube A, 4-1 shuttle valve A, 4-2 Fenton reaction zone water inlet, 5 slender straight tube B, 5-1 regeneration liquid distributor, 5-1.1 liquid addition hole, 5-1.2 Connector, 5-2 Shuttle valve B, 5-3 Regeneration liquid siphon, 6-Fenton reaction zone, 6-1 Sedimentation sludge hopper, 6-2 Sludge discharge pipe, 6-3 Sludge pump, 7 Hydrogen peroxide dosing port, 8 Ferrous ion reagent dosing port, 9 Water injection liquid inlet pipe, 10 U-shaped connecting pipe, 11 Dispersion plate, 12 Fenton reaction zone water outlet, Stop valve 12-1, Filter 12-2, Siphon 12-3, 13 Exhaust observation port, 14 Stirring motor, 14-1 Z-shaped stirring paddle, 15 Acid-base neutralizer dosing port, 16 pH online monitor. DETAILED DESCRIPTION

[0024] The specific embodiments of the present invention are described in detail below in conjunction with the accompanying drawings, but it should be understood that the protection scope of the present invention is not limited by the specific embodiments.

[0025] The specific implementation of the utility model is as follows: Figure 1 shown.

[0026] A device for removing organic matter from fly ash acidic high-salt leaching solution consists of an activated carbon adsorption / regeneration module 3 and a Fenton reaction / precipitation module.

[0027] The activated carbon adsorption / regeneration module 3 comprises an inlet distribution layer 3-1, an activated carbon adsorption layer 3-2, a fiber filter media constant temperature layer 3-3, a capillary effect layer 3-4, and a regeneration liquid distributor 5-1. An activated carbon regeneration liquid outlet 3-1.1 is located on the left side of the bottom-most inlet distribution layer 3-1. This outlet is equipped with a shutoff valve 3-1.2 to regulate and control the discharge of the regeneration liquid. The right side houses the equipment water inlet, which includes a vacuum circulation pump 1. This introduces the treated water source into the equipment through the circulation pump inlet 2, which is connected to the equipment water inlet shutoff valve 2-1, ensuring precise control of the water inlet process. An electric heating tube is located in the center of the fiber filter media constant temperature layer 3-3. These tubes are arranged in a mosquito coil pattern around the heating center 3-3.2. This ensures uniform heating of the solution and provides the necessary heat energy for activated carbon regeneration, optimizing the adsorption and regeneration processes. The inlet distribution layer 3-1 is laid with interlayers of large and small sand and gravel. This structure not only ensures uniform water distribution but also allows the acidic salt solution to escape upward. The regeneration liquid distributor 5-1 is composed of a plurality of small liquid addition holes 5-1.1 connected in a radial disc matrix, and the liquid addition holes 5-1.1 are connected by connectors 5-1.2. The inlet distribution layer 3-1 is located at the bottom, the activated carbon adsorption layer 3-2 is located above the inlet distribution layer 3-1, the fiber filter media constant temperature layer 3-3 is located above the activated carbon adsorption layer 3-2, the capillary effect layer 3-4 is located above the fiber filter media constant temperature layer 3-3, and the regeneration liquid distributor 5-1 is located above the capillary effect layer 3-4.

[0028] The sedimentation area 6 consists of a sedimentation sludge hopper 6-1, a sludge discharge pipe 6-2, and a sludge pump 6-3. The sedimentation sludge hopper 6-1 is the core of the sedimentation area and is designed as a conical structure. The bottom of the sedimentation sludge hopper is connected to the sludge discharge pipe 6-2, which is connected to the sludge pump 6-3.

[0029] The top of the Fenton reaction zone 6 is sealed, with an exhaust observation port 13 on the top. An agitator is installed in the middle of the reaction area. The agitator is driven by a motor 14 and equipped with a Z-shaped stirring paddle 14-1 to achieve efficient mixing of the reaction solution at a controllable rate. The top of the Fenton reaction zone 6 is provided with an acid-base neutralizer dosing port 15 and a pH online monitor 16. The acid-base neutralizer dosing port 15 and the pH online monitor 16 are both deep inside the Fenton reaction zone, ensuring the timeliness and accuracy of pH adjustment, which is crucial for maintaining the optimal conditions of the Fenton reaction and the generation of activated carbon regeneration liquid. A Fenton reaction zone water outlet 12 is provided on the left side of the Fenton reaction zone 6 for discharging the treated liquid. A Fenton reaction dosing device is provided on the left side, and a Fenton reaction zone water inlet 4-2 and an activated carbon regeneration liquid siphon reflux port 5-3 are provided on the right side, and shuttle valves A and B are connected thereto respectively. The Fenton reaction zone 6 is connected to the capillary effect layer 3-4 and the regeneration liquid distributor 5-1 through a slender straight pipe A4 and a slender straight pipe B5. The shuttle valve A is connected to the slender straight pipe A, and the shuttle valve B is connected to the slender straight pipe B. The slender straight pipe A penetrates into the middle of the capillary effect layer, and the slender straight pipe B penetrates into the middle of the regeneration liquid distributor. The opening and closing of the valves are precisely controlled by positive and negative pressure to adjust the flow direction of the solution and ensure the stable operation of the entire treatment system.

[0030] The shuttle valve body consists of one or more hollow cylinders of equal diameter, roughly circular in cross-section to ensure continuous and uniform fluid flow. Openings are located at both the bottom and top ends of the cylinder to facilitate fluid flow. Specifically, the longitudinal cross-sections of the bottom and top ends are designed as isosceles trapezoids. The shuttle valve's core component is a spherical check block, which plays a critical role in valve operation. This spherical design provides excellent sealing performance and flexible movement, enabling precise control of valve opening and closing.

[0031] The water outlet 12 of the Fenton reaction zone 6 consists of a siphon tube 12-3 extending into the middle, a filter 12-2, and a shutoff valve 12-1. The outlet 12 is located outside the tank, while the filter 12-2 is located inside the Fenton reaction zone 6 to filter suspended particles. The shutoff valve 12-1 is located inside the tank and outside the Fenton reaction zone 6, allowing for intermittent water discharge. When the liquid level falls below the bottom of the siphon tube 12-3, water discharge from the Fenton reaction zone 6 ceases. The siphon tube 12-3 extends deep into the Fenton reaction zone 6, with its bottom end positioned just above the sediment hopper 6-1. This design ensures that water discharge automatically ceases when the liquid level in the Fenton reaction zone falls below its bottom end, preventing sediment from being discharged and thus ensuring water quality.

[0032] The Fenton reaction doser includes a hydrogen peroxide dosing port 7, a ferrous ion reagent dosing port 8, a water jet inlet pipe 9, a U-shaped connecting pipe 10, and a disperser 11. The hydrogen peroxide dosing port 7 is connected to the ferrous ion reagent dosing port 8 through the water jet inlet pipe 9, the water jet inlet pipe 9 is connected to the U-shaped connecting pipe 10, and the U-shaped connecting pipe 10 is connected to the disperser 11. The design of the U-shaped connecting pipe 10 not only provides an additional mixing area, but also helps to achieve sufficient mixing reaction of chemical reagents through its U-shaped structure. The disperser 11 is composed of three dispersion disks 11, and the three dispersion disks 11 are located inside the Fenton reaction zone 6. The U-shaped connecting pipe 10 and the water jet inlet pipe 9 are located inside the box and outside the Fenton reaction zone 6. The hydrogen peroxide dosing port 7 and the ferrous ion dosing port 8 are located outside the box. This layout helps to protect these key components and avoid direct contact with the reaction medium, while facilitating monitoring and maintenance by operators. The hydrogen peroxide dosing port 7 and the ferrous ion dosing port 8 are located outside the box, which makes it easier for operators to add and replace chemical reagents while reducing interference with the reaction zone.

[0033] The water inlet 4-2 of the Fenton reaction zone 6 and the activated carbon regeneration liquid siphon reflux port 5-3 are connected by a shuttle valve structure. The shuttle valve structure is composed of a shuttle valve A4-1 and a shuttle valve B 5-2. A check block is provided inside each shuttle valve. The shuttle valve A4-1 is connected to the slender straight pipe A4 and the water inlet 4-2 of the Fenton reaction zone. The shuttle valve B 5-2 is connected to the slender straight pipe B5 and the activated carbon regeneration liquid siphon reflux port 5-3. The shuttle valve B The top of pipe 5-2 is connected to the activated carbon regeneration liquid siphon return port 5-3 via a U-shaped tube. Water inlet 4-2 is located in the middle of the sidewall of shuttle valve A4-1, extending deep into the middle of the Fenton reaction zone. Slender straight pipe A is connected to the bottom of shuttle valve A4-1, and slender straight pipe B is located in the middle of the sidewall of shuttle valve B. Activated carbon regeneration liquid siphon return port 5-3 is equipped with a filter element to intercept fine suspended matter and particulates, protecting subsequent treatment units from contamination. Slender straight pipe A4 extends into the middle of capillary effect layer 3-4. Slender straight pipe B5 is connected to the regeneration liquid distributor 5-1 above capillary effect layer 3-4. Slender straight pipes A and B are arranged parallel to each other.

[0034] like Figure 2As shown, the regeneration liquid distributor 5-1 adopts a radial disc matrix layout and is composed of a plurality of small liquid-adding circular holes 5-1.1. These liquid-adding circular holes are interconnected by connectors 5-1.2, and eight first-layer liquid-adding circular holes 5-1.1 surround the central liquid-adding circular hole 5-1.1. Each first-layer liquid-adding circular hole 5-1.1 radiates outward the same number of secondary liquid-adding circular holes 5-1.1 to form a second layer. In the second layer, an additional liquid-adding circular hole 5-1.1 is provided between every two adjacent secondary liquid-adding circular holes 5-1.1 to optimize the fluid distribution. The six liquid-adding circular holes 5-1.1 in the original first layer continue to expand outward to form the third layer, whose diameter is larger than that of the second layer. This radial expansion maintains a constant number of liquid-adding circular holes after the fourth layer, and the diameter of each layer increases successively until a ten-layer disc matrix structure is formed, ensuring uniform distribution and efficient transmission of the fluid in the distributor.

[0035] like Figure 3 As shown, the heating tube 3-3.1 in the constant temperature zone 3-3 of the fiber filter material is composed of an electric heating tube, and the electric heating tube is distributed around the electric heating center 3-3.2 in a mosquito coil.

[0036] The working process of this utility model: Figure 1 、 Figure 2 and Figure 3 shown.

[0037] Removal of organic matter from fly ash acidic high salt extract: Figure 1 and Figure 2 shown.

[0038] When the equipment is initially started, the relevant control valves and pumps must be in the preset state: the activated carbon regeneration liquid outlet stop valve 3-1.2, the sludge pump 6-3 and the water outlet stop valve 12-1 are all in the closed state, the equipment water inlet stop valve 2-1 is opened, the vacuum circulation pump 1 is turned on, and the fly ash acidic high-salt extract is pressurized and pumped into the water inlet distribution layer 3-1 through the water inlet 2. The large sand and small gravel laid between the layers of the water inlet distribution layer 3-1 realize the upward dispersion of the acidic salt solution, and the acidic salt solution is dispersed through the activated carbon adsorption layer 3-2. The porous adsorption structure of the activated carbon is used to achieve the adsorption and removal of organic matter in the solution. Then the solution penetrates the fiber filter material constant temperature layer 3-3, filters some tiny impurities, and finally enters the capillary effect layer 3-4.

[0039] Due to capillary action, the solution in the slender straight tube A4 extending into the middle of the capillary effect layer 3-4 gradually rises within the tube and enters the shuttle valve A4-1. The check block within the shuttle valve A4-1 is pushed upward by the positive pressure within the tube. At this time, the slender straight tube B5 connected to the capillary effect layer 3-4 also experiences capillary action, but the check block within the connected shuttle valve B5-2 is pushed upward by the pressure within the tube, causing the upper outlets of both shuttle valves A and B to be blocked by the check blocks. The outlet of the regeneration liquid siphon tube 5-3 is closed, and the solution therefore flows only into the Fenton reaction zone 6 through the Fenton reaction zone water inlet 4-2.

[0040] After the acidic high-salt extract enters the Fenton reaction zone through the capillary effect layer, the stirrer motor 13 is turned on and set to a low-speed stirring state of 200 to 500 r / min. The dosing pump of the hydrogen peroxide dosing port 7 and the check valve of the ferrous ion reagent dosing port 8 are opened, and the mass concentration ratio of the ferrous ion reagent to hydrogen peroxide is added to be 1:10 to 1:25. The negative pressure effect generated by the pressurized injection of the hydrogen peroxide reagent is used to inhale the ferrous ion reagent through the pipeline, achieving synchronous flow and preliminary mixing of the two reagents. The two reagents are fully mixed and reacted through the U-shaped connecting pipe 10 to generate a large amount of hydroxyl free radicals, which are then fed into the Fenton reaction zone 6 by the circular dispersion disk of the disperser 11. Under the turbulence of the Z-shaped stirring paddle 14-1, the organic matter is oxidized and degraded by the reaction with the acidic high-salt extract for a reaction time of 30 to 60 minutes. After the organic matter is removed, the stirring motor 13 is set to a medium-high speed stirring state of 800 to 1200 r / min to enhance the mixing effect. Open the stop valve of the acid-base neutralizer dosing port 15, observe the pH value of the acidic salt solution through the pH online monitor, calculate the amount of alkali to be added, and adjust the pH of the solution to 6-9. After the neutralization reaction is completed, turn off the stirring motor 13 and let the system enter the static sedimentation stage. Let it settle for 30 minutes so that the sludge generated by the reaction can be settled into the sedimentation sludge hopper 6-1. Open the water outlet stop valve 12-1 and discharge the solution from the equipment through the siphon 12-3. When the liquid level is lower than the bottom of the siphon, open the sludge pump 6-3 to discharge the remaining precipitated iron sludge from the equipment. At this point, the organic matter removal of the fly ash acidic high-salt extract is completed.

[0041] Activated carbon regeneration: Figure 1 、 Figure 2 and Figure 3 shown.

[0042] In order to ensure the high efficiency of the equipment operation, the activated carbon layer is regenerated after it has worked for 5 to 7 days. When the last batch of acidic high-salt extracts completes the removal of organic matter, no neutralization treatment is performed. The pH value of the solution is monitored at 2.8 to 3.5 by a pH online monitor. If the pH value does not meet this range, the stop valve of the acid-base neutralizer dosing port 15 must be opened immediately. According to the pH monitoring results, an appropriate amount of acid or alkali is accurately added to adjust the pH. The treated solution is retained in the Fenton reaction zone 6. The dosing pump of the hydrogen peroxide dosing port 7 and the check valve of the ferrous ion reagent dosing port 8 are opened. The ferrous ion reagent and hydrogen peroxide are added at a mass concentration ratio of 1:3 to 1:7. The negative pressure effect of the pressurized hydrogen peroxide reagent injected into the pipeline is used to absorb the ferrous ion reagent into the pipeline. The ferrous ion reagent is then fully mixed and reacted in the U-shaped connecting pipe 10. The reaction product is then sent to the Fenton reaction zone through the disperser 11 for stirring and reacting with the solution. The equipment water inlet stop valve 2-1 is closed, and the activated carbon regeneration liquid outlet stop valve 3-1.2 is opened. The liquid level of the capillary effect layer 3-4 drops, resulting in the slender straight pipe A4 and the slender straight pipe B. The liquid level in tube 5 drops. This change causes the check blocks in shuttle valve A4-1 and shuttle valve B5-2 to fall due to gravity, automatically sealing the bottom ends of their respective valves and ensuring that the Fenton reaction zone inlet 4-2 remains closed. The falling liquid level in slender straight tube B5 creates a negative pressure in the regeneration liquid siphon tube 5-3. Consequently, the solution in Fenton reaction zone 6 is filtered through the filter element within the tube and drawn along slender straight tube B5 into the regeneration liquid distributor 5-1. It then radiates through multiple small circular liquid-feeding holes 5-1.2 into the capillary effect layer 3-4 and permeates downward into the fiber filter material constant temperature layer 3-3. The electric heating tube 3-3.1 is activated, set to a temperature of 40-55°C, heating the regeneration liquid before entering the activated carbon layer, where it undergoes regeneration. The regeneration process lasts 30-60 minutes. This completes the generation of regeneration liquid for the activated carbon adsorbent material.

[0043] The above is only a preferred embodiment of the present invention. It should be pointed out that for those skilled in the art, several modifications and improvements can be made without departing from the structure of the present invention. These modifications and improvements will not affect the effect of the implementation of the present invention and the practicality of the patent.

Claims

1. A device for removing organic matter from fly ash acidic high-salt extract, comprising a housing, a Fenton reaction zone, and an activated carbon regeneration / adsorption zone below the Fenton reaction zone, characterized in that: One side of the Fenton reaction zone is connected to a dosing device, and one side is provided with a plurality of shuttle valves. A siphon is provided to penetrate into the Fenton reaction zone, and a sedimentation hopper is located at the bottom of the Fenton reaction zone. The bottom shuttle valve is connected to the slender straight pipe A, and the top shuttle valve is connected to the slender straight pipe B; The activated carbon regeneration / adsorption area is composed of several filter layers, the slender straight tube A penetrates into the capillary effect layer, and the slender straight tube B penetrates into the regeneration liquid distributor.

2. The device for removing organic matter from fly ash acidic high-salt leaching solution according to claim 1, characterized in that: A check block is provided inside each shuttle valve. The top shuttle valve is connected to a regeneration liquid siphon, and the bottom shuttle valve is connected to a water inlet of the Fenton reaction zone.

3. The device for removing organic matter from fly ash acidic high-salt leaching solution according to claim 1, characterized in that: The dosing device comprises a plurality of dosing ports, a water jet liquid inlet pipe and a plurality of dispersion discs. The plurality of dosing ports are connected through the water jet liquid inlet pipe, and the water jet liquid inlet pipe and the plurality of dispersion discs are connected through a U-shaped connecting pipe.

4. The device for removing organic matter from fly ash acidic high-salt leaching solution according to claim 1, 2 or 3, characterized in that: Several dispersion discs in the dosing device extend deep into the Fenton reaction zone.

5. The device for removing organic matter from fly ash acidic high-salt leaching solution according to claim 1, characterized in that: The outlet of the Fenton reaction is connected to a siphon, and the bottom end of the siphon is located above the sedimentation hopper.

6. The device for removing organic matter from fly ash acidic high-salt leaching solution according to claim 1 or 2, characterized in that: An acid-base neutralizer dosing port and a pH online monitor are provided on the top of the Fenton reaction zone.

7. The device for removing organic matter from fly ash acidic high-salt leaching solution according to claim 1 or 2, characterized in that: A sedimentation zone is provided at the bottom of the Fenton reaction zone, including a sedimentation sludge hopper and a sludge discharge pipe connected to the bottom of the sedimentation sludge hopper.

8. The device for removing organic matter from fly ash acidic high-salt leaching solution according to claim 1, characterized in that: The activated carbon regeneration / adsorption zone consists of several filtration layers, and the capillary effect layer is located below the regeneration liquid distributor.

9. The device for removing organic matter from fly ash acidic high-salt leaching solution according to claim 8, characterized in that: The water inlet distribution layer is located at the bottom of several filter layers, one end of which is connected to the activated carbon regeneration liquid outlet and the other end is connected to the equipment water inlet device.

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